EP3466890B1 - Verfahren zur aufbereitung von abwasser aus der milchindustrie - Google Patents

Verfahren zur aufbereitung von abwasser aus der milchindustrie Download PDF

Info

Publication number: EP3466890B1
Authority: EP; European Patent Office
Prior art keywords: permeate; process according; reverse osmosis; waste water; range
Prior art date: 2017-10-05
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.): Active

Application number

EP17194947.2A

Other languages

German (de)

English (en)

French (fr)

Other versions

EP3466890A1 (de

Inventor

Sven-Rainer Döring

Thorben Oehlckers

Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)

DMK Deutsches Milchkontor GmbH

Original Assignee

DMK Deutsches Milchkontor GmbH

Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)

2017-10-05

Filing date

2017-10-05

Publication date

2020-09-02

2017-10-05 Application filed by DMK Deutsches Milchkontor GmbH filed Critical DMK Deutsches Milchkontor GmbH

2017-10-05 Priority to EP17194947.2A priority Critical patent/EP3466890B1/de

2017-10-05 Priority to DK17194947.2T priority patent/DK3466890T3/da

2018-09-20 Priority to CN201811100538.4A priority patent/CN109626624A/zh

2018-10-04 Priority to US16/151,879 priority patent/US11130695B2/en

2019-04-10 Publication of EP3466890A1 publication Critical patent/EP3466890A1/de

2020-09-02 Application granted granted Critical

2020-09-02 Publication of EP3466890B1 publication Critical patent/EP3466890B1/de

Status Active legal-status Critical Current

2037-10-05 Anticipated expiration legal-status Critical

Links

238000000034 method Methods 0.000 title claims description 45
239000002351 wastewater Substances 0.000 title claims description 23
235000013365 dairy product Nutrition 0.000 title claims description 8
238000000746 purification Methods 0.000 title 1
XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 42
JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 claims description 38
239000012528 membrane Substances 0.000 claims description 27
239000012466 permeate Substances 0.000 claims description 27
238000001223 reverse osmosis Methods 0.000 claims description 25
239000004202 carbamide Substances 0.000 claims description 21
239000004310 lactic acid Substances 0.000 claims description 18
235000014655 lactic acid Nutrition 0.000 claims description 18
239000012465 retentate Substances 0.000 claims description 13
230000002378 acidificating effect Effects 0.000 claims description 12
239000011148 porous material Substances 0.000 claims description 12
JVTAAEKCZFNVCJ-UHFFFAOYSA-M Lactate Chemical compound CC(O)C([O-])=O JVTAAEKCZFNVCJ-UHFFFAOYSA-M 0.000 claims description 9
239000008267 milk Substances 0.000 claims description 7
235000013336 milk Nutrition 0.000 claims description 7
210000004080 milk Anatomy 0.000 claims description 7
MKJXYGKVIBWPFZ-UHFFFAOYSA-L calcium lactate Chemical compound [Ca+2].CC(O)C([O-])=O.CC(O)C([O-])=O MKJXYGKVIBWPFZ-UHFFFAOYSA-L 0.000 claims description 2
239000001527 calcium lactate Substances 0.000 claims description 2
235000011086 calcium lactate Nutrition 0.000 claims description 2
229960002401 calcium lactate Drugs 0.000 claims description 2
238000001816 cooling Methods 0.000 claims description 2
239000001521 potassium lactate Substances 0.000 claims description 2
235000011085 potassium lactate Nutrition 0.000 claims description 2
229960001304 potassium lactate Drugs 0.000 claims description 2
238000004064 recycling Methods 0.000 claims description 2
239000001540 sodium lactate Substances 0.000 claims description 2
235000011088 sodium lactate Nutrition 0.000 claims description 2
229940001447 lactate Drugs 0.000 claims 2
CYDQOEWLBCCFJZ-UHFFFAOYSA-N 4-(4-fluorophenyl)oxane-4-carboxylic acid Chemical compound C=1C=C(F)C=CC=1C1(C(=O)O)CCOCC1 CYDQOEWLBCCFJZ-UHFFFAOYSA-N 0.000 claims 1
PHZLMBHDXVLRIX-UHFFFAOYSA-M potassium lactate Chemical compound [K+].CC(O)C([O-])=O PHZLMBHDXVLRIX-UHFFFAOYSA-M 0.000 claims 1
230000001376 precipitating effect Effects 0.000 claims 1
229940005581 sodium lactate Drugs 0.000 claims 1
HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 10
230000003204 osmotic effect Effects 0.000 description 7
XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
239000000463 material Substances 0.000 description 5
230000000717 retained effect Effects 0.000 description 5
238000000926 separation method Methods 0.000 description 5
239000000126 substance Substances 0.000 description 5
239000000243 solution Substances 0.000 description 4
239000005862 Whey Substances 0.000 description 3
102000007544 Whey Proteins Human genes 0.000 description 3
108010046377 Whey Proteins Proteins 0.000 description 3
238000010612 desalination reaction Methods 0.000 description 3
239000004205 dimethyl polysiloxane Substances 0.000 description 3
238000001914 filtration Methods 0.000 description 3
239000004033 plastic Substances 0.000 description 3
229920003023 plastic Polymers 0.000 description 3
229920000435 poly(dimethylsiloxane) Polymers 0.000 description 3
-1 polydimethylsiloxane Polymers 0.000 description 3
238000011084 recovery Methods 0.000 description 3
239000002904 solvent Substances 0.000 description 3
DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
239000003929 acidic solution Substances 0.000 description 2
239000012141 concentrate Substances 0.000 description 2
239000007788 liquid Substances 0.000 description 2
239000010865 sewage Substances 0.000 description 2
150000003384 small molecules Chemical class 0.000 description 2
GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
239000002253 acid Substances 0.000 description 1
150000007513 acids Chemical class 0.000 description 1
QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
239000000920 calcium hydroxide Substances 0.000 description 1
229910001861 calcium hydroxide Inorganic materials 0.000 description 1
238000005352 clarification Methods 0.000 description 1
238000009792 diffusion process Methods 0.000 description 1
239000003651 drinking water Substances 0.000 description 1
235000020188 drinking water Nutrition 0.000 description 1
230000000694 effects Effects 0.000 description 1
238000005516 engineering process Methods 0.000 description 1
238000001704 evaporation Methods 0.000 description 1
230000008020 evaporation Effects 0.000 description 1
239000013505 freshwater Substances 0.000 description 1
239000012535 impurity Substances 0.000 description 1
239000010842 industrial wastewater Substances 0.000 description 1
150000007529 inorganic bases Chemical class 0.000 description 1
229910052500 inorganic mineral Inorganic materials 0.000 description 1
150000002500 ions Chemical class 0.000 description 1
238000004519 manufacturing process Methods 0.000 description 1
230000000813 microbial effect Effects 0.000 description 1
239000011707 mineral Substances 0.000 description 1
235000010755 mineral Nutrition 0.000 description 1
150000007522 mineralic acids Chemical class 0.000 description 1
238000001728 nano-filtration Methods 0.000 description 1
229910017604 nitric acid Inorganic materials 0.000 description 1
239000001301 oxygen Substances 0.000 description 1
229910052760 oxygen Inorganic materials 0.000 description 1
229910052700 potassium Inorganic materials 0.000 description 1
238000001556 precipitation Methods 0.000 description 1
239000000047 product Substances 0.000 description 1
239000013535 sea water Substances 0.000 description 1
229910052708 sodium Inorganic materials 0.000 description 1
229940083542 sodium Drugs 0.000 description 1
238000001694 spray drying Methods 0.000 description 1
239000002352 surface water Substances 0.000 description 1
239000003643 water by type Substances 0.000 description 1

Images

Classifications

- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/22—Treatment of water, waste water, or sewage by freezing
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
- C02F2103/327—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from processes relating to the production of dairy products
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions

Definitions

the invention is in the field of the dairy industry and relates to a method for treating waste water polluted with organic load.
lactic acid typically: 0.03 to 0.1% by weight
urea typically: 0.5 to 2.0 mg / kg
the object of the invention was therefore to purify wastewater contaminated with lactic acid and urea and having a COD in the range of 500 and above as easily and continuously as possible to a COD less than 50 and in particular less than 10, so that the wastewater does not disposed of or clarified industrially, but can be returned directly to process steps within the dairy industry.
a correspondingly contaminated wastewater is first adjusted to a basic pH value with a lye, whereby lactate is precipitated. This is separated off as retentate in a first reverse osmosis, whereby the COD value is already reduced to about half of the original value.
the permeate which still contains urea, is adjusted to an acidic pH value by adding an inorganic acid, cooled to 2 to 10 ° C. and placed on a second reverse osmosis membrane with the same pore diameter.
the pH shift is a critical feature, since lactate is only precipitated in an alkaline medium; in acidic conditions, the lactate would be converted back into soluble lactic acid, while the pore constriction of the osmosis membrane requires an acidic environment.
the present invention specifically relates to wastewater that occurs in the course of processing milk and the production of milk products.
wastewater is wastewater from concentration and membrane processes, especially during the evaporation and spray drying of milk fractions and filtration steps, such as reverse osmosis, since these contain lactic acid and urea as the main organic load and are difficult to separate completely together.
Wastewater of this type generally has a COD value of about 500 and above, the proportion of lactic acid and urea together making up at least 90% by weight and typically about 92 to 98% by weight of the total organic load.
the method according to the invention described below is divided into two steps, namely the separation of the lactic acid and the separation of the urea.
the wastewater to be treated is first adjusted to a basic pH value, preferably in the range from about 9 to about 11 and preferably about 10, to separate the lactic acid.
Inorganic bases can be used for this, in particular concentrated sodium or potassium hydroxide solution, possibly also calcium hydroxide. Through this measure, the lactic acid is precipitated as sodium, potassium or calcium lactate.
Reverse osmosis or reverse osmosis is a physical membrane process for the concentration of substances dissolved in liquids, in which the natural osmosis process is reversed with pressure.
the principle of the process is that the medium in which the concentration of a certain substance is to be reduced is separated from the medium in which the concentration is to be increased by a semi-permeable membrane. This is exposed to a pressure that has to be higher than the pressure created by the osmotic desire to balance the concentration. This allows the molecules of the solvent to migrate against their "natural" osmotic direction of propagation. The process pushes them into the compartment where dissolved substances are less concentrated. Typical pressures for reverse osmosis are in the range from 3 to 30 bar (drinking water desalination) or up to 80 bar (sea water desalination).
the osmotic membrane which only allows the carrier liquid (solvent) through and holds back the dissolved substances (solutes), must be able to withstand these high pressures. If the pressure difference more than compensates for the osmotic gradient, the solvent molecules will fit through the membrane like a filter, while the "impurity molecules" are retained. In contrast to a classic membrane filter, osmosis membranes do not have continuous pores. Rather, the ions and molecules migrate through the membrane by diffusing through the membrane material, as described by the solution-diffusion model: the osmotic pressure increases with increasing concentration difference. If the osmotic pressure equals the applied pressure, the process comes to a standstill. There is then an osmotic equilibrium. A steady drainage of the concentrate can prevent this. At the concentrate outlet, the pressure is either controlled by a pressure regulator or used by a pressure exchanger to build up the pressure required in the system inlet.
the first RO step can take place both in the cold and in the heat, i.e. at a temperature in the range of about 8 to 25 ° C and preferably 10 to 12 ° C or about 25 to 55 ° C and especially 30 to 40 ° C. Temperatures around 25 ° C have proven to be particularly advantageous, since here there is a good balance between a sufficiently high flow on the one hand and low microbial load and clogging of the membrane on the other.
the membranes which are preferably plastic membranes, have an average pore diameter in the range from approximately 50 to approximately 500 Daltons and in particular approximately 100 to approximately 200 Daltons.
the method is designed to produce as little retentate as possible, so the first reverse osmosis is preferably carried out with a concentration factor in the range from approximately 10 to approximately 100 and in particular approximately 40 to 60.
the lactate is quantitatively retained as retentate, while the permeate already has about half of its COD load, i.e. has lost its organic load and now, based on 500, typically have COD values in the range of only 250.
the first permeate obtained in this way is adjusted to an acidic pH, preferably in the range from about 2 to 3.
Mineral acids such as hydrochloric acid or nitric acid are particularly suitable for this purpose.
the acidic permeate is cooled to 2 to 10 ° C, preferably about 3 to 5 ° C. This can take place, for example, in that the reverse osmosis membrane is correspondingly cooled, namely by process water from a heat exchanger step.
the membranes which are preferably plastic membranes, have an average pore diameter in the range from about 50 to about 500 Daltons and in particular from about 100 to about 200 Daltons and are therefore too large to retain small molecules such as urea .
the osmosis membranes especially those made of plastics, contract under acidic conditions and at the same time low temperature and thus now also enable quantitative separation of the urea.
the second reverse osmosis is also preferably carried out with a concentration factor in the range from about 10 to about 100 and in particular about 40 to 60.
the urea is also retained quantitatively as retentate, and a second permeate is obtained, which has a COD value of less than 50, generally from about 1 to about 10.
the two reverse osmosis steps can be reversed and first the urea and then the lactic acid can be separated without this having a negative effect on the final COD value achieved.
the wastewater treated in this way has COD values of typically 5 and is practically fresh water quality and can be reused as such in processes in the milk processing industry, for example as slide water in filtration steps or as discharge to the surface water.
1,000 liters of vapor condensate from sour whey recovery with a COD value of around 500 and a lactic acid content of around 0.08% by weight and a quantity of urea of around 1 mg / kg were placed in a stirred kettle and adjusted to a pH value of 11 with sodium hydroxide solution set.
the solution was stirred at about 20 ° C. for about 10 minutes and then applied to a first reverse osmosis membrane (material: polydimethylsiloxane) with an average pore size of 100 daltons; the concentration factor was 40. 25 liters of lactic acid-containing retentate and 975 liters of permeate were obtained, which had a COD value of only 250.
the permeate was adjusted to pH 3 with hydrochloric acid in a second stirred kettle and stirred at about 20 ° C. for about 10 minutes.
the acidic solution was then placed on a second reverse osmosis membrane (material: PES), which also had an average pore size of 100 Dalton and had been cooled to 3 ° C. by process water from a heat exchanger step. 25 liters of urea-containing retentate and 950 liters of permeate were obtained, which still had a COD value of 5.
Vapor condensates from sour whey recovery with a COD value of about 500 according to Example 1 were passed through a flow pipe and continuously mixed with aqueous 50% by weight sodium hydroxide solution via a first rotor-stator mixer, so that a pH of 11 was established.
the basic stream was applied to a first reverse osmosis membrane (material: polydimethylsiloxane) with an average pore size of 100 Dalton; the concentration factor was 40. While the retentate was being retained, the permeate was passed on and adjusted to a pH of 3 with hydrochloric acid via a second rotor-stator mixer.
the acidic solution was continuously applied to a second reverse osmosis membrane (material: polydimethylsiloxane), which also had an average pore size of 100 Dalton and had been cooled to 3 ° C. by process water from a heat exchanger step. While the retentate was again retained, a clarified wastewater was continuously removed as permeate, which still had a COD value of 5.
a second reverse osmosis membrane material: polydimethylsiloxane

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Life Sciences & Earth Sciences (AREA)
Hydrology & Water Resources (AREA)
Engineering & Computer Science (AREA)
Environmental & Geological Engineering (AREA)
Water Supply & Treatment (AREA)
Chemical & Material Sciences (AREA)
Organic Chemistry (AREA)
Separation Using Semi-Permeable Membranes (AREA)

EP17194947.2A 2017-10-05 2017-10-05 Verfahren zur aufbereitung von abwasser aus der milchindustrie Active EP3466890B1 (de)

Priority Applications (4)

Application Number	Priority Date	Filing Date	Title
EP17194947.2A EP3466890B1 (de)	2017-10-05	2017-10-05	Verfahren zur aufbereitung von abwasser aus der milchindustrie
DK17194947.2T DK3466890T3 (da)	2017-10-05	2017-10-05	Fremgangsmåde til rensning af spildevand fra mælkeindustrien
CN201811100538.4A CN109626624A (zh)	2017-10-05	2018-09-20	用于处理源自乳品加工的废水的方法
US16/151,879 US11130695B2 (en)	2017-10-05	2018-10-04	Process for purification of waste water from dairy processing

Applications Claiming Priority (1)

Application Number	Priority Date	Filing Date	Title
EP17194947.2A EP3466890B1 (de)	2017-10-05	2017-10-05	Verfahren zur aufbereitung von abwasser aus der milchindustrie

Publications (2)

Publication Number	Publication Date
EP3466890A1 EP3466890A1 (de)	2019-04-10
EP3466890B1 true EP3466890B1 (de)	2020-09-02

Family

ID=60021991

Family Applications (1)

Application Number	Title	Priority Date	Filing Date
EP17194947.2A Active EP3466890B1 (de)	2017-10-05	2017-10-05	Verfahren zur aufbereitung von abwasser aus der milchindustrie

Country Status (4)

Country	Link
US (1)	US11130695B2 (da)
EP (1)	EP3466890B1 (da)
CN (1)	CN109626624A (da)
DK (1)	DK3466890T3 (da)

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Publication number	Priority date	Publication date	Assignee	Title
DE102020126428A1 (de)	2020-10-08	2022-04-14	Milkron GmbH	Verfahren zur Herstellung eines Käseprodukts sowie Verfahren zur Aufbereitung einer Salz enthaltenden Lake
CN114804387A (zh) *	2022-05-06	2022-07-29	四川绿沃创新环保工程有限公司	一种乳酸蒸发冷凝水回收的方法

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number	Priority date	Publication date	Assignee	Title
US2071368A (en) *	1935-12-28	1937-02-23	Sealtest System Lab Inc	Process of making lactate salts and lactic acid
JP2000281638A (ja) *	1999-03-26	2000-10-10	Snow Brand Milk Prod Co Ltd	尿素の分離方法
FR2806172B1 (fr) *	2000-03-07	2002-05-10	Eastman Kodak Co	Procede et dispositif pour le traitement d'un film photographique inversible couleur
FI115919B (fi) *	2002-06-27	2005-08-15	Danisco Sweeteners Oy	Menetelmä kiteytysinhibiittoreiden poistamiseksi monosakkaridisokeriliuoksista
JP5487617B2 (ja) *	2007-06-29	2014-05-07	東レ株式会社	乳酸の製造方法
CN102869619B (zh) *	2010-04-30	2016-03-02	栗田工业株式会社	水处理方法和超纯水制造方法
JP2013043860A (ja) *	2011-08-24	2013-03-04	Hitachi Plant Technologies Ltd	精製乳酸の製造方法
US10377645B2 (en) *	2012-08-31	2019-08-13	University Of Puerto Rico	Urea-based system for energy and waste recovery in water recycling
US9695066B2 (en) *	2014-01-31	2017-07-04	Paragon Space Development Corporation	Ionomer-membrane water processing apparatus
AT515878B1 (de)	2014-05-28	2019-09-15	Dr Wett Bernhard	Verfahren zur Abwasserklärung
JP6641628B2 (ja) *	2014-09-05	2020-02-05	東レ株式会社	糖液の製造方法
US10642940B2 (en)	2016-02-05	2020-05-05	Microsoft Technology Licensing, Llc	Configurable access to a document's revision history

2017
- 2017-10-05 DK DK17194947.2T patent/DK3466890T3/da active
- 2017-10-05 EP EP17194947.2A patent/EP3466890B1/de active Active
2018
- 2018-09-20 CN CN201811100538.4A patent/CN109626624A/zh active Pending
- 2018-10-04 US US16/151,879 patent/US11130695B2/en active Active

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* Cited by examiner, † Cited by third party
Title
None *

Also Published As

Publication number	Publication date
US11130695B2 (en)	2021-09-28
US20190106344A1 (en)	2019-04-11
EP3466890A1 (de)	2019-04-10
CN109626624A (zh)	2019-04-16
DK3466890T3 (da)	2020-10-19

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